Process and apparatus for separating no2 from a co2 and no2-containing fluid

ABSTRACT

A process for separating carbon dioxide from a fluid containing carbon dioxide, NO 2 , and at least one of oxygen, argon, and nitrogen comprises the steps of separating at least part of the fluid into a carbon dioxide enriched stream, a carbon dioxide depleted stream comprising CO 2  and at least one of oxygen, argon, and nitrogen and a NO 2  enriched stream and recycling said NO 2  enriched stream upstream of the separation step.

CROSS-REFERENCE TO RELATED APPLICATIONS

The present application is a divisional application of U.S. applicationSer. No. 14/265,710, filed Apr. 30, 2014, which claims the benefit ofpriority under 35 U.S.C. §119 (e) to U.S. Provisional Patent ApplicationNo. 61/971,840, filed Mar. 28, 2014, the entire contents of which areincorporated herein by reference.

BACKGROUND

1. Field of the Invention

The present invention relates to a process and apparatus for theseparation of gaseous mixture containing carbon dioxide as maincomponent. It relates in particular to processes and apparatus forpurifying carbon dioxide, for example coming from combustion of a carboncontaining fuel, such as takes place in an oxycombustion fossil fuel orbiomass power plant.

2. Related Art

The combustion of carbon containing fuels produces CO₂ and gases such asSO₂, SO₃, and NOx which pollute the atmosphere and which are majorcontributors to the greenhouse effect—especially CO₂. These CO₂emissions are concentrated in four main sectors: power generation,industrial processes, transportation, and residential or commercialbuildings. Most of the emissions of CO₂ to the atmosphere from theelectricity generation and industrial sectors are currently in the formof flue gas from combustion, in which the CO₂ concentration is typically4-14% by volume for air-fired combustion or up to 60-70% by volume foroxy-combustion, although CO₂ is produced at high concentrations by a fewindustrial processes.

In principle, the flue gas could be purified and stored in which case itwould have to be compressed to a pressure of typically more than 100 barabs, a pressure that would consume an excessive amount of energy.Systems for recovering and purifying CO₂ from flue gas are sometimesreferred to as CO₂ purification units or CPUs. For these reasons it ispreferable to produce relatively high purity stream of CO₂ fortransport, onsite consumption, or storage. This carbon dioxide could beused for enhanced oil recovery or just injected in depleted gas and oilfields or in aquifers.

Among the numerous issues that CO₂ capture faces today, the purity ofCO₂ sent to sub-surface storage (EOR or geological sequestration) is oneof the more delicate to address. This is due to the huge difficulties toclearly understand and model the interactions between sub-surfaceelements and injected gases as well as piping corrosion.

One type of acidic gas commonly found in CO₂ captured from flue gas isNOx. By NOx, we mean one or more of oxides of nitrogen, including NO,N₂O, N₂O₄, and NO₂ and N₂O₃. Below 158° C., NO₂ is in equilibrium withits polymer/dimer N₂O₄ where the lower the temperature, the higher theconcentration of N₂O₄ is compared to NO₂. In this document, the word NO₂is used to mean not only NO₂ but also its polymer/dimer N₂O₄ inequilibrium.

NOx compounds are not necessarily removed in the CPU process. Someapplications, however, require NOx-free CO₂.

Some have proposed removal of NOx from flue gas using a De-NOx columnthrough separation of NO₂ from CO₂ as the critical temperature of NO₂ ishigher than that of CO₂. The use of a De-NOx column still presents thechallenge of dealing with the NO₂-enriched fluid of the liquid bottom.For example, U.S. Pat. No. 7,708,804 proposes the use of De-NOx columnwhere the NO₂-enriched liquid from the bottom of the De-NOx column isdealt with in one of three ways. First, it may be recycled to the inletof the compressor. Second, it may be sent to a wash column. Third, itmay be burned at the burner associated with a boiler (which may itselfbe the source of the flue gas) in an attempt to reduce the NO₂ to N₂.

With regard to the first technique, recycling the NO₂-enriched fluid tothe inlet of the compressor is disadvantageous. Because the recyclestream may represent about 5-10% of the total flow compressed andtreated downstream of the compressor, the compressor and downstreamequipment must be sized 5-10% larger than it would have to be if theNO₂-enriched stream was otherwise not recycled. There would also be a 5%to 10% increase in the required compression energy. Furthermore, therelatively higher acid gas content of the flue gas being compressed willproduce a greater amount of acid gas condensate in the compressors.Therefore the compressors and driers will be subjected to a more severeacidic attack in comparison to the absence of a NO₂ recycle stream. Thismore acidic attack may lead to a decreased useful lifetime for thecompressors or require the compressor to be constructed of a more costlymaterial that is sufficiently resistant to such acid fluids. Similarnegative impacts upon the driers would be expected to occur due to thepresence of the acid gas. Finally, in order to decrease the amount ofNO2 being recycled to the compressor, the reflux liquid flow rate to theDe-NOx column may be decreased. However, a decrease in the reflux liquidflow rate to the De-NOx column may soon cause the column to exceed itswettability limit. This will lead to unsatisfactory decreases indistillation efficiency.

Therefore, it is one object of the invention to provide a method andsystem of CO₂ purification from flue gas that does not require therecycling of a NO₂-enriched fluid to a point upstream in thepurification process.

With regard to the second technique, use of a wash column would resultin significant CO2 losses in case the washed stream is not recycled atthe CPU inlet. If the washed stream is instead recycled the at CPUinlet, significant CO₂ losses may be avoided. However, this suffers thesame above drawback of increasing the size of the compressor anddownstream equipment to accommodate the increased flow rate.

Therefore, it is another object of the invention to provide a method andsystem of CO₂ purification from flue gas that does not require the useof a wash column for removal of NO₂ from the bottom of a De-NOx column.

With regard to the third technique, reduction of NO₂ in the flame of aburner on the scale of a NO₂-enriched stream from a De-NOx columnpresents a very technically challenging problem. Regardless of therelative state of development for such an approach, reduction of NOx inthe burner flame still results in significant CO₂ losses.

Thus, it is an object of the invention to provide a more reliable way toproduce a CO₂ product from purification of flue gas that contains asatisfactorily low amount of NOx.

SUMMARY OF THE INVENTION

There is disclosed a process for separating NO₂ from a CO₂ andNO₂-containing fluid. The process comprises the following steps. Thefluid comprising CO₂, NO₂, and at least one of oxygen, argon, andnitrogen is fed to a rectifying distillation column. A first gaseousstream is withdrawn from the rectifying column that is enriched in CO₂and deficient in NO₂ relative to the fluid comprising CO₂, NO₂, and atleast one of oxygen, argon, and nitrogen. A liquid stream is withdrawnfrom the rectifying column that is enriched in NO₂ relative to the fluidcomprising CO₂, NO₂, and at least one of oxygen, argon, and nitrogen.The NO₂-enriched liquid stream is fed to a fluid separation membrane. Asecond gaseous stream comprising a permeate gas is withdrawn from themembrane that is enriched in NO₂ and deficient in CO₂ relative to theliquid stream fed to the membrane. A non-permeate liquid stream iswithdrawn from the membrane that is deficient in NO₂ and enriched in CO₂relative to the liquid stream fed to the membrane. The non-permeateliquid stream is recycled to the rectifying column.

There is also disclosed an apparatus for separating NO₂ from a CO₂ andNO₂-containing fluid, comprising: a source of a fluid comprising NO₂ andCO₂; a rectifying distillation column receiving the source fluid; afluid separation membrane that receives a liquid stream from therectifying column and yields a liquid non-permeate stream and a gaseouspermeate stream; and a pump feeding, to the rectifying column, thenon-permeate liquid from the membrane.

Either or both of the process and apparatus may include one or more ofthe following aspects:

-   -   the fluid comprising CO₂, NO₂, and at least one of oxygen,        argon, and nitrogen is produced by compressing flue gas at a        compressor followed by drying and at least partial condensation        of the compressed flue gas at a heat exchanger.    -   the first gaseous stream is at least partially condensed at a        heat exchanger; the at least partially condensed stream is        separated at a phase separator to produce a third gaseous stream        enriched in at least one of oxygen, argon and nitrogen relative        to the first gaseous stream and a liquid stream enriched in CO₂        relative to the first gaseous stream; the liquid stream enriched        in CO₂ is fed to a stripping column; a fourth gaseous stream        withdrawn from the stripping column is fed to a suction inlet of        the compressor; and a liquid product CO₂ stream is withdrawn        from the stripping column.    -   the liquid product CO₂ stream is expanded to provide a biphasic        product CO₂ stream; any liquid component in the biphasic product        CO₂ stream is vaporized at a heat exchanger to provide a wholly        gaseous product CO₂ stream; and the wholly gaseous product CO₂        stream us compressed and heated to provide a supercritical        product CO₂ stream.    -   a sweep gas is fed to the fluid separation membrane, wherein the        second gaseous stream further comprises the sweep gas.    -   the second gaseous stream is fed to a wash column to dissolve at        least some of the NO₂ present in the second gaseous stream and        form nitric acid.    -   a fuel is combusted with an oxidant in a boiler to produce the        fuel gas, wherein the flue gas has a NO_(x) content greater than        300 ppm.    -   a separation layer of the fluid separation membrane comprises a        material selected from the group consisting of: a cross-linked        polysiloxane copolyether, polyurethane-polyether block        copolymer, a poly(urea)-poly(ether) block copolymer, a        poly(ester)-poly(ether) block copolymer, and a        poly(amide)-poly(ether) block copolymer.    -   a heat exchanger at least partially condenses a gaseous stream        from the rectifying column; a phase separator receives the at        least partially condensed stream from the heat exchanger and        produces a gaseous stream comprising a majority of N₂, O₂,        and/or Ar and a liquid stream comprising a majority of CO₂; a        stripping distillation column receives the liquid stream        comprising a majority of CO₂ from the phase separator, the        stripping column being adapted and configured to separate the        contents of the liquid stream comprising a majority of CO₂ into        a gaseous stream and a liquid CO₂ product stream.    -   a compressor and a drying unit are adapted and configured to        compress and dry the source fluid, wherein the heat exchanger is        also adapted and configured to at least partially condense the        compressed and dried source fluid prior to being fed to the        rectifying column.    -   the fluid source is a boiler adapted and configured to produce        flue gas and the flue gas is the fluid comprising NO₂ and CO₂.    -   the compressor also receives the gaseous stream from the        stripping column.    -   a compressor and heater compresses and heats the wholly gaseous        CO₂ product stream to provide a supercritical product CO₂        stream.    -   the membrane also receives the sweep gas on a permeate side of        the membrane.    -   a wash column receives the gaseous permeate stream and dissolves        at least some of the NO₂ present in gaseous permeate stream to        form nitric acid.    -   the membrane includes a separation layer comprising a material        selected from the group consisting of: a cross-linked        polysiloxane copolyether, polyurethane-polyether block        copolymer, a poly(urea)-poly(ether) block copolymer, a        poly(ester)-poly(ether) block copolymer, and a        poly(amide)-poly(ether) block copolymer.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1 is a schematic view of an oxycombustion plant.

FIG. 2 is a schematic view of a compression and purification unit.

FIG. 3 shows a low temperature purification unit.

DETAILED DESCRIPTION OF THE INVENTION

The invention will now be described in further detail with reference tothe figures.

FIG. 1 is a schematic view of an oxycombustion plant. Air separationunit 2 produces an oxygen stream 10 at a typical purity of 95-98 mol. %and a waste nitrogen stream 13. Oxygen stream 10 is split into two substreams 11 and 12. The primary flue gas recycle stream 15 passes throughcoal mills 3 where coal 14 is pulverized. Substream 11 is mixed with therecycle stream downstream of the coal mills 3 and the mixture isintroduced in the burners of the boiler 1. Sub stream 12 is mixed withsecondary flue gas recycle stream 16 which provides the additionalballast to the burners to maintain temperatures within the furnace atacceptable levels. Water stream(s) is introduced in the boiler 1 inorder to produce steam stream(s) 18 which is expanded in steam turbine8.

One of ordinary skill in the art will recognize that the flue gas to betreated according to the invention may instead be derived from any ofwell-known oxy-combustion schemes differing from the one illustrated inFIG. 1.

Flue gas stream 19 rich in CO₂, typically containing more than 70 mol. %on a dry basis, goes through several treatments to remove someimpurities. Unit 4 is NOx removing system such as a selective catalystreduction unit (SCR). Unit 5 is a dust removal system such aselectrostatic precipitator and/or baghouse filters. Unit 6 is adesulfurization system adapted and configured to remove SO₂ and/or SO₃.Units 4 and 6 may not be necessary depending on the CO₂ productspecification. Flue gas stream 24 is then introduced in a compressionand purification unit 7 in order to produce a high CO₂ purity stream 25suitable for transport, injection into a pipeline, use in enhanced oilrecovery, and/or sequestration in a geologic formation. Unit 7 alsoproduces a waste stream 26.

While the flue gas of FIG. 1 is derived from oxy-combustion, one ofordinary skill in the art will recognize that a lowered NOx CO₂ productmay also be produced from flue gas derived from air-fired combustion oroxygen-enriched combustion.

FIG. 2 is a schematic view of a compression and purification unit whichcould be used as unit 7 in FIG. 1. Flue gas stream 110 (corresponding tostream 24 of FIG. 1) enters a low pressure pretreatment unit 101 whereit is prepared for compression unit 102. This unit could include, forexample, among other steps:

-   -   a dust removal step in a wet scrubber and/or a dry process        either dynamic, such as pulse-jet cartridges or static, such as        pockets and cartridges;    -   a (further) desulfurization step in a wet scrubber with water        and/or soda ash or caustic soda injection; and    -   a cooling step in order to minimize the flow through water        condensation and the power of compression unit both due to flow        and temperature reduction.

Waste stream(s) 111 could include condensed water, dust and dissolvedspecies like H₂SO₄, HNO₃, Na₂SO₄, CaSO₄, Na₂CO₃, and CaCO.

Compression unit 102 compresses stream 112 from a pressure close toatmospheric pressure to a high pressure typically between 15 and 60 barabs, preferably around 30 bar abs. This compression could be done inseveral stages with intermediate cooling. In this case, somecondensate(s) 113 could be produced. Such condensate(s) 113 typicallyincludes HNO₃ formed from reaction of NO₂ and water. Heat of compressionmay be usefully recovered in the intermediate cooling step, for example,in preheating boiler feed water. Hot stream 114 leaves the compressionunit 102 and enters a high pressure pretreatment unit 103.

The high pressure pretreatment unit 103 includes at least:

-   -   one or several cooling step(s) in order to decrease the        temperature and decrease the water content; and    -   a drying step to remove most of the water, for example by        adsorption.

The high pressure pretreatment unit 103 could also include, but is notlimited to:

-   -   a high pressure washing column for cooling and/or purification;        and    -   a mercury removal step.

Effluents from unit 103 include gaseous stream 115 (the regenerationstream of the drying step) and may include liquid stream(s) 116/117(from the cooling step and/or the high pressure washing column).

The stream 114 may contain NO₂. In this case, it is sometimes preferableto remove the NO₂ by adsorption upstream of the unit 104. In this case,the stream 114 may be treated by adsorption and the regeneration gasused to regenerate the adsorbent is removed having a content enriched inNO₂ with respect to that of stream 114. The gaseous stream 115 mayoptionally be recycled at least in part upstream of the compression unit102, upstream of the pretreatment unit 101 or to the boiler 1 of thecombustion unit.

Unit 104 is a low temperature purification unit. In this case, lowtemperature means a minimum temperature in the process cycle for thepurification of the flue gas below 0° C. and preferably below −20° C. asclose as possible to the triple point temperature of pure CO₂ at −56.6°C. In this unit, stream 118 is cooled down and partially condensed inone (or several steps). One (or several) liquid phase stream(s) enrichedin CO₂ is (are) recovered, expanded and vaporized in order to have aproduct enriched in CO₂ 119. Such gaseous CO2 product may be usedon-site. Alternatively, the recovered liquid phase stream(s) enriched inCO₂ may be maintained in liquid form and the pressure and temperatureadjusted according to known techniques to provide a liquid product CO₂stream suitable for storage, on-site consumption, or transport by tubetrailer. As another alternative, the pressure and temperature of therecovered liquid phase stream(s) enriched in CO₂ may be adjustedaccording to known techniques to provide a supercritical product CO₂stream suitable for injection into a pipeline or sequestered in ageologic formation. One (or several) incondensible high pressurestream(s) 120 is (are) recovered and could be expanded in an expander.

Unit 104 includes a rectifying distillation column that separates a NO₂and CO₂-containing feed fluid into a CO₂-enriched gaseous stream and aNO₂-enriched liquid stream (relative to the concentrations of NO₂ andCO₂ in the feed fluid). The feed fluid can consist of stream 118 or maybe derived from stream 118 after further treatment of stream 118.

Unit 104 also includes a fluid separation membrane (operated underpervaporative conditions) that separates the NO₂-enriched liquid streamfrom the rectifying column into a NO₂-enriched gaseous permeate streamand a liquid non-permeate stream. The liquid non-permeate stream isrecycled to the rectifying column.

Unit 104 also includes phase separator that expands the CO₂-enrichedgaseous stream from the rectifying column and separates it into agaseous stream (for eventual venting) and a liquid stream for feeding toa stripping distillation column (which also receives a stripping fluidderived from vaporization of at least a portion of the liquidnon-permeate stream). The distillation column strips the incondensablecomponents (O₂, N₂, and Ar) from the combined contents of the strippingfluid and the liquid stream (from the phase separator) into a gaseousstream and the liquid phase stream(s) enriched in CO₂. The gaseousstream from the stripping column may be combined with the feed fluid fedto the rectifying column.

CO₂ enriched product 119 may be further treated to provide it inwhichever forms (gaseous, liquid, supercritical, solid) andpressure/temperature desired. In the case of sequestration, CO2 enrichedproduct 119 may be further compressed condensed and then furthercompressed with a pump in order to be delivered at high pressure(typically 100 to 200 bar abs) for injection into a pipeline leading tothe sequestration site.

FIG. 3 shows a low temperature purification unit that could be used asunit 104 in FIG. 2. At least one process according to the inventionoperates within such a unit.

Stream 118 comprising flue gas at around 30 bar and at a temperature ofbetween 15° C. and 43° C. contains mainly carbon dioxide but alsoincludes lesser amounts of NO₂, oxygen, argon and nitrogen. The actualamount of NOx will vary over time depending upon how much NOx hasalready been adsorbed in the driers. Typically, the inlet NOx will varybetween 0 ppm and 500 ppm. The actual amount of NOx will also dependupon the type of burner producing the flue gas. Stream 118 may beproduced by unit 103 already at the desired pressure conditions or itmay be brought up to the desired pressure level using optionalcompressor 124. Compressed flue gas stream 127 is alternatingly directedto one of two driers 129, 131. While one of the driers 129, 131 is beingoperated to dry stream 127, the other of the driers is regenerated.

Dried, compressed flue gas stream 133 is cooled and at least partiallycondensed at multi-fluid heat exchanger 135.

The liquid or biphasic flue gas stream 137 is fed to rectifying (alsoknown as De-NOx) column 139 as reflux and separated into a NO₂-enrichedliquid stream 141 and a CO₂-enriched gaseous stream 143. The pressure inthe De NOx column is typically about 25 bar abs where the inlet gastemperature is about −19° C.

The NO₂-enriched liquid stream 141 is fed to a feed gas side of apervaporative separation membrane 147. The membrane 147 includes aseparation layer that is comprised of a material that selectivelypermeates NO₂ (and SO₂, if present) over CO₂ so as to provide aNO₂-enriched permeate and a CO₂-enriched non-permeate. An optional sweepgas 145 fed to a permeation side (opposite that of the feed gas side) ofmembrane 147 will enhance permeation of the NO₂ from stream 141 acrossthe membrane 147 from the feed gas side to the permeation side bylowering its partial pressure on the permeate side. The combined sweepgas 145 and NO₂-enriched permeate is withdrawn from membrane 147 asstream 149.

The CO₂-enriched non-permeate withdrawn from membrane 147 as liquidstream 151 is pressurized with pump 153. The pressurized liquid stream155 is combined with stream 192 and recycled back to rectifying column139.

Gaseous stream 143, containing between about 1-5 ppm NO₂ and about 98%CO₂, is cooled and at least partially condensed at heat exchanger 135 toprovide a cool biphasic stream 161. Biphasic stream 161 is then fed to aphase separator 163 to provide a N₂, O₂, and Ar-enriched gaseous stream165 and a CO₂-enriched liquid stream 167.

Stream 165 is warmed at heat exchanger 135 and the warmed stream 169further warmed at heater or heat exchanger 171. Twice-warmed stream 171is used to regenerate the drier 129, 131 being operated in regenerationmode and then subsequently warmed at heat exchanger 177 in order enhancethe available expansion energy recovered at expander 179. Downstream ofexpander 179, it is warmed at heat exchanger 135 and the warmed,expanded stream 120 vented.

The pressure of the CO₂-enriched liquid stream 167 is decreased atexpansion valve and fed as reflux to stripping column 186. Column 186,under a pressure around 15 bar and a temperature between −27° C. and−50° C., operates to remove the incondensible components (N₂, O₂, andAr) in the form of a CO₂-depleted gaseous stream 187 from the top ofcolumn 186. Some of the cold energy of stream 187 is recovered at heatexchanger 135, thereby providing warmed stream 189 which is combinedwith flue gas stream 118 at the suction inlet of compressor 124.

A carbon dioxide liquid stream 191 is also removed from the bottom ofcolumn 186 and split into stream 192, stream 194, and stream 196. Stream192 is combined with the liquid non-permeate stream 155 to providestream 157 which is fed to the rectifying column 139. The pressure ofstream 194 is reduced at expansion valve 193 to provide a cooler,biphasic (liquid/gaseous CO₂) stream 195. Latent heat in stream 195 isrecovered at heat exchanger 135 through vaporization of the remainingliquid phase of biphasic stream 195 to provide gaseous stream 197.

The CO₂ in stream 196 is warmed in two portions at heat exchanger 135 todifferent degrees. Resultant stream 198 is superheated while stream 200remains at its dewpoint and is fed to stripping column 186 for providingthe necessary heat to the column.

Stream 197 and stream 198 are then combined at the suction inlet ofcompressor 199, compressed at compressor 199 and cooled at heatexchanger 201 to a level above the critical pressure of CO₂. Thepressure of the heated, compressed stream is then raised above thecritical pressure of CO₂ to provide supercritical CO₂-enriched productstream 119 useful for injection into a pipeline.

One of ordinary skill in the art will recognize that the CO₂-enrichedproduct 119 may instead be provided in liquid form for storage, on-siteconsumption, and/or transport by tube trailer. Also, the liquid CO₂stream 191 need not be fed to expansion valve 193 or passed through heatexchanger 135. Indeed, the pressure and/or temperature of liquid CO₂stream 191 may be adjusted according to techniques well-known in the artto provide any desired pressure and temperature for a liquidCO₂-enriched product 119.

The membrane 147 includes a perm-selective separation layer that isprimarily responsible for the separation of NO₂ (along with SO₂ ifpresent) and CO₂. The membrane 147 may be made entirely of the polymericmaterial of the separation layer. The membrane 147 may instead have acomposite structure where the separation layer is supported by a supportlayer whose purpose is to provide mechanical strength. The material ofthe support layer may be any material known to those skilled in the artof fluid membrane separation as having relatively high flux andsufficiently desirable mechanical strength. The membrane 147 may haveany configuration known to those skilled in the art of fluid separationmembranes, including spirally-wound sheets and hollow fibers.

The membrane 147 operates on a solubility selectivity principle.Solubility is usually correlated with molecular parameters such as theLennard-Jones affinity constant or the critical temperature. Since thecritical temperatures of NO₂ and SO₂ are above 157° C. and the criticaltemperature of CO₂ is only 30.98° C., we believe that NO₂ and SO₂ areexpected to exhibit high permeability through polymers with flexiblemain chains and having polar affinity.

Several polymeric materials are suitable for use in the separation layerof the membrane 147, including polysiloxane copolyethers (which arecross-linked), polyurethane-polyether block copolymers,poly(urea)-poly(ether) block copolymers, poly(ester)-poly(ether) blockcopolymers, and poly(amide)-poly(ether) block copolymers.

In the case of a cross-linked polysiloxane copolyether, it comprisespolysiloxane copolyether comprises a polymeric chain comprisingrepeating units of the molecular segment of formula (1), a terminalmolecular segment —O—W bonded to a silicon atom of one end of the chainwhere O is an oxygen atom, and a terminal molecular segment —W bonded toan oxygen atom of the other end of the chain:

Each W is selected from the group consisting of a —Si(CH₃)₃ group, themolecular segment of formula (2), the molecular segment of formula (3),and the molecular segment of formula (4);

Each X comprises b repeating units of the molecular segment of formula(5) and c repeating units of the molecular segment of formula (6):

Each R is individually selected from the group consisting of a phenylgroup, a C₁-C₆ alkyl group, the molecular segment of formula (2), themolecular segment of formula (3), and the molecular segment of formula(4);

In order to ensure the presence of a polyether content in thepolysiloxane copolyether, the following two conditions apply. First, ifeach W is a —Si(CH₃)₃ group or the molecular segment of formula (3),then at least some R's are the molecular segment of formula (2) or themolecular segment of formula (4). Second, if each R is either a phenylgroup or a C₁-C₆ alkyl group, then each W is either the molecularsegment of formula (2) or the molecular segment of formula (4).

The following integers have the following ranges:

-   -   p: 1-3;    -   q: 1-3;    -   b: 0-400;    -   c: 0-200.        The number of repeating units where R is a C₁-C₆ alkyl group is        1-2000.

The ratio of polyether segments to polysiloxane segments may vary. WhenW is —Si(CH₃)₃ group, cross-linking sites are present in the middle ofthe chain and the ratio of the number of molecular segments that are ofeither formulae (5) or (6) to the number of silicon atoms in the chainranges from about 0.05 to about 6.0. When each R is either a phenylgroup or a C₁-C₆ alkyl group, cross-linking sites are present at eachend of the chain and the ratio of the number of molecular segments thatare of either formulae (5) or (6) to the number of silicon atoms in thechain ranges from about 0.05 to about 0.33. In this case, a greatercontent of siloxane-based repeating units is desired for providinggreater robustness.

A potential cross-linking site may be wherever either W or R is themolecular segment of formulae (2), (3), or (4). The type of linkageformed at the cross-linked site will depend upon the W or R in questionand the type of cross-linking agent or cross-linking promoter. For W'sand R's of the molecular segment of formula (2), a urethane linkage maybe formed using a monomeric diisocyanate, a monomeric triisocyanate orpolymeric isocyanate cross-linking agent. For W's and R's of themolecular segment of formula (3), a urea linkage may be formed using amonomeric diisocyanate, a monomeric triisocyanate or polymericisocyanate cross-linking agent. For W's and R's of the molecular segmentof formula (3), an amide linkage may instead be formed using a di-acylchloride substituted aromatic cross-linking agent, or a tri-acylchloride substituted aromatic cross-linking agent. For W's and R's ofthe molecular segment of formula (4), the copolymer may be cross-linkedusing a free radical cross-linking promoter, such as an azo or peroxidefree radical initiator.

Non-limiting examples of suitable monomeric diisocyanate, monomerictriisocyanate or polymeric isocyanate cross-linking agents are toluenediisocyanate (TDI) commercially available from a wide variety of sourcesor cyanate-functionalized siloxanes commercially available from Siltech.Non-limiting examples of suitable di-acyl chloride substituted aromaticcross-linking agents and tri-acyl chloride substituted aromaticcross-linking agents include 1,3-benzenedicarbonyl dichloride,1,4-benzenedicarbonlyl dichloride, and 1,3,5-benzenetricarbonyltrichloride.

The cross-linked polysiloxane copolyether may optionally be cross-linkedtogether with one or more silicone elastomers. The silicone elastomermay be derived from a first silicone polymer having a first reactivefunctional group (such as a vinylsiloxane unit) and a crosslinking agenthaving a second reactive functional group (such as a hydrogensiloxaneunit). Suitable silicone elastomers may be commercially obtained fromMomentive under trade name RTV615 and from Dow Corning under trade nameSylgard 184,182, or 186.

Particularly suitable types of polysiloxane copolyethers may becommercially obtained from Siltech under the trade names D-208, Di-2510,Di-5018F, Di1010, and J-1015-O.

The polyurethane-polyether block copolymers are produced by reacting atleast one polyether glycol with either an aromatic or aliphaticdiisocyanate followed by reaction with at least one aliphatic diol (toform a polyurethane-polyether) or with a at least one aliphatic diamine(to form a polyurea-polyether) in the presence of a catalyst, such asorganotin compounds, such as dibutyltindilaurate, but other catalystsknown to one skilled in the art may be used. The resulting polymerscontain the soft segments of formula (I_(s)) comprising polyether andthe hard segments of formula (I_(h)) comprising polyurethane orpolyurea.

The resultant polyurethane-polyether or polyurea-polyether blockcopolymers are represented by the repeating units of formulas (I_(s))and (I_(h)):

R_(i) of formulas (I_(s)) and (I_(h)) is an aliphatic or aromaticradical of at least about 2-18 carbon atoms. (PE) is a polyether segmenthaving a number average molecular weight, M_(n) (which is essentiallyequivalent to M_(n) of the repeating formula (I_(a))), ranging fromabout 600 to 8000, and preferably about 1000 to 4000. R_(a) of (I_(h))is a linear or branched aliphatic radical of at least about 2-18 carbonatoms; and, X is an oxygen atom or —NH—. If X is oxygen, the blockcopolymer is a polyurethane-polyether, and if X is —NH—, the blockcopolymer is a polyurea-polyether. Within the block copolymer, thenumber of carbon atoms in the repeating units may vary and there may bevarieties and combinations of numbers of carbon atoms therein. Thenumber average molecular weight of the repeating formula (I_(h)) ispreferably in the range of about 200 to 3000, and more preferably about200-1000. In one copolymer in particular, Ri is linear —(CH₂)₆—, or amoiety of composition selected from the group primarily comprisingformula (S), formula (T), formula (U), or (V) below, and a combinationor mixtures thereof.

These structures correspond to 1,6-hexanediisocyanate,tolylene-2,6-diisocyanate, tolylene-2,4-diisocyanate,1,3-xylylenediisocyanate, and 4,4′-methylenebis (phenylisocyanate),respectively. The polyether segment, (PE), is derived preferably from apolyether glycol of number average molecular weight of about 600-8000,and more preferably about 1000-4000, and preferably an oxygen/carbonratio of about 0.2-0.5. Preferred polyether glycols are hydroxylterminated polyethylene glycol, hydroxyl terminated 1,2-polypropyleneglycol, and hydroxyl terminated 1,4-polybutylene glycol, although otherglycols known or used by one skilled in the art may be used.

The hard segment of the polyurethane-polyether or polyurea-polyetherblock copolymer is derived from the reaction of residual aliphatic oraromatic diisocyanate end groups or monomer with either at least onealiphatic diol or at least one aliphatic diamine. Preferred diols ordiamines contain at least about 2-18 carbon atoms and can be linear orbranched. Most preferred are diols or diamines containing at least about2-6 carbon atoms. Typical diols and diamines are ethylene glycol,1,3-propanediol, 1,2-propanediol, 1,4-butanediol, 1,6-hexanediol,1,2-diaminoethane, 1,4-diaminobutane, 1,5-diaminopentane,1,5-diaminohexane, 1,6-diaminohexane, and dI-serine(3-amino-2-hydroxypropionic acid), although other diols and diaminesknown or used by one skilled in the art may be used. Typically, thepolyurethane-polyether or polyurea-polyether block copolymers exhibit anumber average molecular weight in the range from about 23,000 to400,000 and preferably about 50,000-280,000. As shown from the varietyof combinations of components, a wide range and variety of types ofpolyurethane-polyether and polyurea-polyether block copolymers arecontemplated and disclosed herein. Typically, the soft segment comprisesabout 50-90 weight percent of the block copolymer weight, and moretypically, about 60-85 percent.

The polyester-polyether block copolymers are produced by reacting atleast one hydroxyl terminated polyether glycol, an excess of at leastone aliphatic diol, and at least one dicarboxylic ester of an aromaticor aliphatic diacid in the presence of a catalyst. The resultingpolymers contain the soft segments of formula (II_(s)) comprisingpolyether and the hard segments of formula (II_(h)) comprisingpolyester:

R_(a) of (II_(s)) and (II_(h)) is an aliphatic or aromatic radical ofabout at least 2-18 carbon atoms. (PE) of (II_(s)) is a polyethersegment having a number average molecular weight, M_(n) (which isessentially equivalent to M_(n) of the repeating formula (II_(s))),ranging from about 600 to 8000, and preferably about 1000 to 4000. R_(d)of (II_(h)) is at least one linear or branched aliphatic radical ofabout at least 2-18 carbon atoms. Within the polyester-polyether blockcopolymer, the number of carbon atoms in the repeating units may varyand there may be varieties and combinations of numbers of carbon atomstherein. The average molecular weight of the repeating formula (II_(h))is preferably in the range of about 200 to 3000, and more preferablyabout 200-1000. In a preferred embodiment of the invention, R_(a) is amoiety of composition selected from the group consisting or comprisingformulas (S), (T), (U), (V), (W), (X), or (Y) below, or a combination ormixture thereof:

Further, where formula (Y) is present or included, the —Z— in formula(Y) is a moiety selected from the group comprising or consisting offormulas (A), (B), (C), or (D), below, or a mixture or combinationthereof:

The polyether segment, (PE), of the polyester-polyether block copolymeris derived preferably from a polyether glycol of number averagemolecular weight of about 600-8000, and more preferably about 1000-4000,and preferably an oxygen/carbon ratio of about 0.2-0.5. Preferredpolyether glycols are hydroxyl terminated polyethylene glycol, hydroxylterminated 1,2-polypropylene glycol, and hydroxyl terminated1,4-polybutylene glycol, although other glycols known or used by oneskilled in the art may be used. The hard segment of the block copolymeris derived from the condensation polymerization of at least one ester ofan aromatic or aliphatic diacid with at least one aliphatic diol. Themoiety R d of formula (I h) is a derivative of the aliphatic diol.Preferred diols contain at least about 2-18 carbon atoms and can belinear and/or branched. Most preferred are diols containing betweenabout 2-6 carbon atoms. Typical diols are ethylene glycol,1,3-propanediol, 1,2-propanediol, 1,4-butanediol, and 1,6-hexanediol,although other diols known or used by one skilled in the art may beused. Typically, the polymers of this invention exhibit a number averagemolecular weight in the range from about 23,000 to 400,000 andpreferably about 50,000-280,000. As shown from the variety ofcombinations of components, a variety of types of polyester-polyetherblock copolymers are contemplated and disclosed herein.

Typically, the soft segment of the polyester-polyether block copolymercomprises about 50-90 weight percent of the copolymer weight, and moretypically, about 60-85 percent.

The polyamide-polyether block copolymers comprise repeating units of themoiety of formula III:

where PA is a saturated aliphatic polyamide segment and PE is apolyether segment. Typically, the saturated aliphatic polyamide segmentis either:

-   -   Nylon 6 (PA6) which is poly[imino(1-oxohexamethylene)], or    -   Nylon 12 (PA12) which is poly[imino(1-oxododecamethylene)].        Typically, the polyether segment is either:    -   PEO which is poly(ethylene oxide), or    -   PTMEO which poly(tetramethylene oxide).        One particularly suitable group of polyamide-polyether block        copolymers is commercially available from Arkema under the        tradename PEBAX. These are obtained by polycondensation of a        carboxylic acid polyamide (PA6, PA11, PA12) with an alcohol        terminated polyether such as poly(tetramethyleneglycol) (PTMG)        or polyethyleneglycol (PEG).

While the invention has been described in conjunction with specificembodiments thereof, it is evident that many alternatives,modifications, and variations will be apparent to those skilled in theart in light of the foregoing description. Accordingly, it is intendedto embrace all such alternatives, modifications, and variations as fallwithin the spirit and broad scope of the appended claims. The presentinvention may suitably comprise, consist or consist essentially of theelements disclosed and may be practiced in the absence of an element notdisclosed. Furthermore, if there is language referring to order, such asfirst and second, it should be understood in an exemplary sense and notin a limiting sense. For example, it can be recognized by those skilledin the art that certain steps can be combined into a single step.

The singular forms “a”, “an” and “the” include plural referents, unlessthe context clearly dictates otherwise.

“Comprising” in a claim is an open transitional term which means thesubsequently identified claim elements are a nonexclusive listing i.e.anything else may be additionally included and remain within the scopeof “comprising.” “Comprising” is defined herein as necessarilyencompassing the more limited transitional terms “consisting essentiallyof” and “consisting of”; “comprising” may therefore be replaced by“consisting essentially of” or “consisting of” and remain within theexpressly defined scope of “comprising”.

“Providing” in a claim is defined to mean furnishing, supplying, makingavailable, or preparing something. The step may be performed by anyactor in the absence of express language in the claim to the contrary.

Optional or optionally means that the subsequently described event orcircumstances may or may not occur. The description includes instanceswhere the event or circumstance occurs and instances where it does notoccur.

Ranges may be expressed herein as from about one particular value,and/or to about another particular value. When such a range isexpressed, it is to be understood that another embodiment is from theone particular value and/or to the other particular value, along withall combinations within said range.

All references identified herein are each hereby incorporated byreference into this application in their entireties, as well as for thespecific information for which each is cited.

What is claimed is:
 1. An apparatus for separating NO₂ from a CO₂ andNO₂-containing fluid, comprising: a source of a fluid comprising NO₂ andCO₂; a rectifying distillation column receiving the source fluid; afluid separation membrane that receives a liquid stream from therectifying column and yields a liquid non-permeate stream and a gaseouspermeate stream; and a pump feeding, to the rectifying column, thenon-permeate liquid from the membrane.
 2. The apparatus of claim 1,further comprising: a heat exchanger at least partially condensing agaseous stream from the rectifying column; a phase separator receivingthe at least partially condensed stream from the heat exchanger andproducing a gaseous stream comprising a majority of N₂, O₂, and/or Arand a liquid stream comprising a majority of CO₂; a strippingdistillation column receiving the liquid stream comprising a majority ofCO2 from the phase separator, the stripping column being adapted andconfigured to separate the contents of the liquid stream comprising amajority of CO₂ into a gaseous stream and a liquid CO₂ product stream.3. The apparatus of claim 2, further comprising a compressor and adrying unit adapted and configured to compress and dry the source fluid,wherein the heat exchanger is also adapted and configured to at leastpartially condense the compressed and dried source fluid prior to beingfed to the rectifying column.
 4. The apparatus of claim 3, wherein thefluid source is a boiler adapted and configured to produce flue gas andthe flue gas is the fluid comprising NO₂ and CO₂.
 5. The apparatus ofclaim 3, wherein the compressor also receives the gaseous stream fromthe stripping column.
 6. The apparatus of claim 3, further comprising acompressor and heater that compress and heats the wholly gaseous CO₂product stream to provide a supercritical product CO₂ stream.
 7. Theprocess of claim 1, further comprising a source of a sweep gas, themembrane also receiving the sweep gas on a permeate side of themembrane.
 8. The apparatus of claim 1, further comprising a wash columnreceiving the gaseous permeate stream and dissolving at least some ofthe NO₂ present in gaseous permeate stream to form nitric acid.
 9. Theapparatus of claim 1, wherein the membrane includes a separation layercomprising a material selected from the group consisting of: across-linked polysiloxane copolyether, polyurethane-polyether blockcopolymer, a poly(urea)-poly(ether) block copolymer, apoly(ester)-poly(ether) block copolymer, and a poly(amide)-poly(ether)block copolymer.